Automated method and system for recovering protein powder meal, omega 3 oil and purified distilled water from animal tissue

ABSTRACT

The present invention describes a method and an automatic system for recovering protein powder meal, crude and pure omega-3 oil and purified distilled water from a mixture of animal tissue processed in a filter-drier-reaction tank. Animal tissue, for example fish, and organic solvent are directly or indirectly fed into the filter-drier-reaction tank. The filter-drier-reaction tank mixes, heats, and separates solid and heavy liquid portions of the mixture, the organic solvents are automatically recycled back in to the system after distillation. The solid portion is retained in the filter-drier-reaction tank and baked. Solid protein powder product (the protein powder meal) is thus recovered.

CROSS-REFERENCES TO RELATED APPLICATIONS

The instant application is a continuation of U.S. patent applicationSer. No. 16/014,844, filed Jun. 21, 2018, which is a continuation ofU.S. patent application Ser. No. 15/803,115, filed Nov. 3, 2017, nowU.S. Pat. No. 10,039,299, which is a divisional of U.S. patentapplication Ser. No. 14/052,514, filed Oct. 11, 2013, now U.S. Pat. No.9,826,757, which claims priority to U.S. Provisional Patent ApplicationNo. 61/794,301 filed Mar. 15, 2013, each of which are herebyincorporated by reference in their entirety for all purposes as if fullyset forth herein.

Reference is made to co-pending U.S. application Ser. No. 11/973,106filed Oct. 5, 2007, published as US 2009/0092737 on Apr. 9, 2009,titled, “METHOD FOR DERIVING A HIGH-PROTEIN POWDER/OMEGA 3 OIL ANDDOUBLE DISTILLED WATER FROM ANY KIND OF FISH OR ANIMAL (PROTEIN),”sharing a common assignee with the instant application, and incorporatedherein by reference.

Reference also is made to co-pending U.S. application Ser. No.12/639,946 filed Dec. 16, 2009, published as US 2010/0189874 on Jul. 29,2010, titled “SYSTEMS AND METHODS FOR DERIVING PROTEIN POWDER,” sharinga common assignee with the instant application, and incorporated hereinby reference.

BACKGROUND OF THE INVENTION Field of the Invention

The present invention generally relates to an automated method and asystem for recovering protein powder meal, crude and pure omega-3 oiland purified distilled water, all from animal tissue, such as a varietyof fish species and/or fish parts. The protein powder meal is referredas solid protein produce or solid product herein, and the three termsare used interchangeable throughout. The system of the present inventionis also known as “SEAVIOR SYSTEM.”

Crude omega-3 oil is obtained after extracting and separating the solidsfrom the liquids and oils from the entire fish and it's parts. Thiscrude omega-3 oil is valuable and has a variety of applications. Crudeomega-3 oil can be further processed to obtain pure omega-3 oil. Pureomega-3 oil means high purity omega-3 oil that is suitable for humanconsumption. For example, pure omega-3 oil can include about 80%, 85%,90%, 95%, 96%, 97%, 98%, 99%, 99.5%, or 99.9% of omega-3 oil. The termscrude omega-3 oil, pure omega-3 oil and omega-3 oil are usedinterchangeable throughout. Purified distilled water means high puritywater that is suitable for human consumption. The terms purifieddistilled water and water are used interchangeable throughout. Therecovered protein powder meal, omega-3 oil and purified water can beused in many fields, for example, as main ingredients in foodmanufacturing, nutrition products, hunger relief packages, cosmetics andhigh quality pet food. It should be noted that the method and system ofthe present invention can be employed with any animal tissue, althoughpreferably, the method and system is used in conjunction with almost anyfish and fish bi-catch and recyclable fresh fish parts, as it is aplentiful and sustainable resource.

More specifically, given the mounting world food shortage problems inmany areas of the globe, the present invention provides a methodologyfor producing a high quality protein supplement, which can provide ameans to combatting the ever growing malnutrition crisis. The proteinsupplement can be derived from a wide variety of optional 100% naturalresources, such as small short lived fresh and plentiful ocean fishwhich are considered green and sustainable and is an excellent renewablenatural resource and it's use will combat overfishing of certain speciesand help balance the oceanic eco system, in addition to the discardedfresh fish parts carcasses generated by the fish processing industries.Environmental benefits are realized by recycling these otherwisediscarded fresh fish materials in the method associated with the currentinvention. In an age where there is a growing requirement for green(i.e. environmentally conscious) processing, the ability to reuse andrecycle fresh and nutritionally valuable waste materials generated bythe general fishery industry affords a certain uniqueness to the currentinvention.

Discussion of the Related Art

Malnutrition is an issue in developing countries with inadequatetechniques and resources for storing perishable foods. Namely, moderntechnological advances, such as refrigeration systems, come at a pricefew can afford in remote, impoverished areas.

While water may be one of earth's most abundant resources, obtainingpurified drinking water still poses a challenge for millions of peopleliving in developing countries. One reason may be attributed to theproximity to available water sources, e.g., landlocked countries andcountries in proximity to bodies of salt water, but not fresh water.Even if proximity is of no concern, financial constraints in developingcountries may result in the lack of readily available, efficient waterpurification systems.

One alternative is to extract vital resources from animal tissue.Whether landlocked or next to the sea, many developing countries have anabundant supply of land or marine animals. Marine animals, morespecifically fish, are made up of resources including protein, fish oilsincluding omega-3, and water derived from the fish itself. In view ofthe techniques employed to recover these products, the shelf-life can beextended. By so doing, the necessity to preserve perishable goods viarefrigeration is reduced and/or eliminated.

While animal tissue purification systems and techniques already exist inthe marketplace, one major setback is the efficiency in recoveringproducts. Inefficiencies generally are attributed to downtime caused byequipment maintenance and replacement. For example, equipment inlets andoutlets, as well as conduits for transferring product, may becomeclogged. Also, employing many pieces of equipment in the purificationsystem requires additional operator time to individually inspect eachpiece of equipment prior to verifying the system is appropriate forfurther processing. What is desired in the art is a more efficientsystem and process for purifying animal tissue to meet present consumerdemands. Also desired is a system and process for improving yield ofrecovered products from animal tissue. Further desired is a system andprocess for recovering products with long shelf-lives.

What is further desired is a solvent recycling system that recycles theorganic solvent and thus reduces the usage of the organic solvent andthe emission of organic solvent (also referred as volatile organiccompound (VOC)) into the atmosphere.

SUMMARY OF THE INVENTION

The present invention proposes a unique and first of a kind technologyto produce a highly pure and stable protein powder meal which is furthersupplemented with levels of desirable minerals such as calcium,potassium, zinc and other required inorganic materials. Theseconstituents are naturally derived from bones and flesh that areassociated with, for example, raw fish ingredients. The resultantprotein powder meal is a complete food source comprising a completeaminogram, whose composition is further complemented by naturallyoccurring inorganic mineral substances. The nature of the technologyutilizes pharmaceutical type processing systems and unit operations toensure final protein product purity and compliance with requirementsthat are imposed in a regulated industry.

An objective of the present invention is to provide a more efficientsystem and method for recovering products from animal tissue. The animaltissue can be raw fish. The raw fish can be any kind of fish and anypart of the fish, including sustainable abundant species of fish andfish parts that is ordinarily considered waste.

Another objective of the present invention is to provide a system andmethod that improves yield of recovered products.

Yet another objective of the present invention is to provide a systemand method that improves shelf-life of the recovered products.

A further objective of the present invention is to provide a system andmethod that recycles the organic solvent and reduces emission of VOCgases into the atmosphere.

The present invention can be considered a general recycling process forfish carcasses and related materials that are discarded daily byfacilities in the fish processing industry. The resultant recycling ofthe otherwise discarded materials to produce a high quality proteinproduct (also referred as “protein powder meal,” used interchangeableherein) realizes a green and sustainable process that reduces the burdenon the environment.

In one aspect of the present invention, an improved system and methodfor recovering products from animal tissue is described. Specifically,the technique involves combining animal tissue and organic solvent insufficient proportions to produce a mixture thereof. The mixture isagitated, heated and filtered in a tank to produce protein powder meal.Preferably, the tank is a single unitary structure. Also recovered isanimal oil and water derived from the animal. In a preferred embodiment,the animal tissue is fish, and the recovered products includes fishprotein, fish oils and water derived from the fish. In an exemplaryembodiment, the solid protein (also referred as “protein powder meal,”used interchangeable herein) is transferred to a mill for furtherprocessing into a powder. In a yet another exemplary embodiment, afiltered, liquid portion of the mixture is filtered to separate fish oilfrom water. In a further embodiment, the portion of the mixture retainedin the single unitary structure after filtration is combined withrecycled organic solvent. The recycled organic solvent is recovered fromthe liquid portion of the mixture.

In another aspect of the present invention, there is described a systemfor recovering products from animal tissue. Preferably, the animaltissue is fish. The system includes a filter-dryer reaction tankincluding one or more inputs and outputs. Animal tissue feedstock andorganic solvent are independently, or collectively, fed into thefilter-dryer reaction tank. The filter-dryer-reaction tank mixes, heatsand filters a mixture containing animal tissue and organic solvent. Thefilter-dryer reaction tank includes an output for removing filtrate, aswell as an output for removing solid product.

BRIEF DESCRIPTION OF THE DRAWINGS

The accompanying drawings, which are incorporated herein and constitutea part of this specification, illustrate embodiments of the inventionand together with the description serve to explain the principles of theinvention.

In the Drawings:

FIG. 1 is an illustration of the present invention in accordance withexemplary embodiments of the present invention;

FIG. 2 is a cross-sectional view of a filter-dryer-reaction tank inaccordance with exemplary embodiments of the present invention; and

FIG. 3 illustrates a recovery system for recovering protein powder meal,omega-3 oil and purified water in detail in accordance with exemplaryembodiments of the present invention.

FIG. 4 illustrates functional hierarchy associated with the automationand control system network for the plant level unit operations are forcontrolling and operating the protein manufacturing plant in detail inaccordance with exemplary embodiments of the present invention.

FIG. 5 illustrates the SA95 object model hierarchy associated with theEnterprise Resource Planning (ERP) system that depicts a verticaltransaction model between the detailed production systems and corporateplanning systems in detail in accordance with exemplary embodiments ofthe present invention.

It will be apparent to those skilled in the art that variousmodifications and variations can be made to the present inventionwithout departing from the spirit or scope of the invention. Thus, it isintended that the present invention cover the modifications andvariations of this invention provided they come within the scope of theappended claims and their equivalents.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

The present invention describes a novel system and process for improvingthe efficiency of recovering products from animal tissue. Also describedis a novel system and process for improving throughput, especially yieldof solid protein, based upon the initial feed of animal tissue. Furtherdescribed in the present invention is a system and process for reducingthe emission of VOC gases into the atmosphere during the processing ofanimal tissue.

Generally, condensing plural pieces of manufacturing equipment into asingle unitary structure has been shown by the inventors to reducedowntime caused by material flow obstructions occurring at multiplelocations in the system. Namely, material flow obstructions occur mostfrequently at inputs and outputs of manufacturing equipment. Materialflow obstructions also occur within conduits connecting different piecesof manufacturing equipment. According to the inventors, processinganimal tissue feedstock in a single filter-dryer-reaction tank torecover a wet cake including solid protein significantly improvesdowntime attributed to maintenance and repair. In addition, the currentunitary invention is a highly automated process; more energy efficient;and requires less manpower than a system comprising multiple unitoperations. Another advantage directly attributed to employing theabove-mentioned system is a reduction in capital and operational costsassociated with procuring and maintaining fewer pieces of equipment. Yetanother advantage realized by the inventors is an improvement in yieldof solid protein and shelf-life, derived from the wet cake by employingthe system and method described herein.

The novel system and process will be discussed in greater detail belowin view of the exemplary, non-limiting embodiments of the presentinvention. Each of the embodiments discussed hereinafter, unlessexpressly noted otherwise, are combinable and envisaged within the scopeof the present invention. It is also understood that the embodiments,while preferred, are exemplary, and those of ordinary skilled in the artwill understand certain modifications to the embodiments are possiblewithout departing from the spirit of the invention.

System

FIG. 1 is a block diagram illustrating an exemplary embodiment of arecovery system 100 according to a first aspect of the presentinvention. According to FIG. 1, the recovery system 100 includes ananimal tissue feedstock 101 for introducing animal tissue. The animaltissue feedstock may be contained within a storage tank. The storagetank may be temperature controlled. Alternatively, the animal tissue maybe housed in a cold room and conveyed downstream for processing eithermanually by technicians, or by any combination of automatic machineryincluding but not limited to screw conveyers, conduits/tubes, pumps,blowers, etc. In an exemplary embodiment, 304SS piping may be employedthroughout the system. In another exemplary embodiment, a pumpconstructed of stainless steel may be employed to assist withtransferring animal tissue downstream.

The recovery system 100 also includes an organic solvent feed 102 forintroducing organic solvent. The organic solvent feed 102 may becontained within a storage tank. The storage tank may have a flat bottomand/or a closed top. The storage tank may also include a leveltransmitter. The level transmitter preferably is constructed fromstainless steel. The tanks may include ports which directly orindirectly communicate with an inlet of nitrogen gas. The storage tankmay also include a conservation valve, butterfly valve, and/or diaphragmvalve. The organic solvent may be delivered downstream by anycombination of equipment including but not limited to piping, pumps,blowers, or the like, as described above. The pump may be stainlesssteel and centrifugal. Piping may be employed as necessary forinterconnecting the process unit operation and downstream equipment.

The present invention involves a highly scalable process and is capableof yielding protein powder and omega 3 oils ranging from lower to higherquantities. The inventive process is also reconfigurable in thatparallel trains of systems can be implemented for concurrent productionrequirements.

Of particular importance, the recovery system 100 also includes asingle, unitary, integrated filter-dryer-reactor tank 110 (referred toas “the FDR tank” hereinafter) which receives animal tissue and organicsolvent for processing. The FDR tank 110 includes vacuum and heatingmodules. The FDR tank also includes a filter for separating solids fromheavy liquids. The FDR tank 110 also comprises one or more agitationdevices that agitate or stir the animal tissue feedstock and solventmixture, as well as a drying module for yielding dry solid proteinproduct once separated from the liquid component (i.e., the water, oil,solvent). Preferably, the FDR tank 110 is constructed of stainless steeland is of a sanitary design. The FDR tank 110 will be described ingreater detail below with reference to FIG. 2.

The recovery system also includes a solid product recovery system 160and a solvent/liquid recycle (SLR) system 170, as illustrated in FIG. 1.The SLR system 170 may include one or more filtrate recovery tanks.Preferably, the filtrate recovery tanks are made of stainless steel. Thefiltrate tanks may include one or more ports which directly orindirectly communicate with an inlet for feeding nitrogen gas thereto.The nitrogen blanket maintains the organic solvent in a nonvolatilestate. The SLR system 170 will be described in greater detail below withreference to FIG. 3.

FIG. 2 is a cross-sectional view of the FDR tank 110 (also indicated byreference numeral 200 and used interchangeably throughout). The FDR tank200 is an externally heated metal vessel, with agitation systems,capable of withstanding elevated pressures and vacuum compression vesselmade of metal. Preferably the metal is selected from alloys suitable forsanitary processing requirements. More preferably, the metal isstainless steel. In another, exemplary embodiment, the FDR tank 200generally is a monolithic or unitary structure capable of beingpressurized and withstanding high levels of vacuum. That is, the FDRtank 200 is machined as a single piece rather than a collection ofdevices connected via conduits.

The FDR tank 200 may include a port 215 communicating directly orindirectly with a feed line for introducing animal tissue from theanimal tissue feedstock 201 and/or a port 216 communicating directly orindirectly with a feed line for introducing organic solvent from theorganic solvent feed 202. Ozone, preferably, is fed from an ozonegenerator 225 which may be located upstream or downstream of the animaltissue feed 201. The FDR tank 200 may also include a port 218communicating directly or indirectly with a VOC recycling system thatwill be discussed later in detail. The FDR tank 200 also includes a port219 communicating directly or indirectly with a solid product recoverytank 260, which is generally illustrated as “solid product recovery 160”in FIG. 1. The FDR tank 200 further includes a discharge port 217communicating directly or directly with the Solvent/Liquid Recyclesystem (SLR system) 270 (which is identified in FIG. 1 as Solvent/LiquidRecycle System 170). Specifically, the SLR system recovers products fromanimal tissue including animal oils and water derived from the animalitself. The SLR system 270 also recovers organic solvent which may berecycled through the system according to user preferences. The FDR tank200 may include a pump, a check valve (CV-01), and an isolation valvebetween the discharge port 217 and the SLR system 270. The check valve(CV-01) can prevent a reverse flow of liquid back from the SLR system270 into the FDR tank 200.

Surrounding the FDR tank 200 is a heater system 220. In an exemplaryembodiment, the outer walls and bottom of the FDR tank 200 aresurrounded by a conventional heating jacket containing a heating medium.Generally, the heating medium is steam or alternative heating transferfluid. Preferably, a steam boiler capable of operating at 6 MMBTU isemployed.

The FDR tank 200 may include a primary agitator assembly 230. Theprimary agitator assembly 230 is located partially inside and partiallyoutside the FDR tank 200. The agitator assembly 230 may include a drivemeans 231, which is, at least in part, preferably located outside of theFDR tank 200. In an exemplary embodiment, the drive means 231 is locatedon or above the FDR tank 200. The drive means 231 rotates a vertical, ornear vertical shaft 232 which is located in or substantially within thethe FDR tank 200. The shaft 232 may be rotated, clockwise orcounterclockwise, at variable speeds as determined by the operator. Therotation speeds have a variable range. The shaft 232 includes one ormore arms 233 with corresponding blades 234 extending there from, whichfacilitate movement of the feedstock and solvent mixture within the FDRtank 200. The movement helps to ensure uniform heating and drying. Theone or more arms 233 may be located at equal or non-equal distances fromeach another in the vertical and/or horizontal plane extending radiallyin the direction of the inner wall of the the FDR tank 200. Each of theone or more blades 234 located on the one or more arms 233 also radiallyextends in the direction of the inner wall of the FDR tank 200 and isconfigured to rotate around the shaft axis. The one or more blades 234may be located at equal or non-equal distances from each other. Theblades 234 may take on a number of shapes; however, the blades arepreferably rectangular or substantially rectangular. Further, the blades234 may include a radially inner portion that is substantially flat andlies substantially in a vertical plane. Alternatively, the blades 234may lie with a positive or a negative pitch. In yet another exemplaryembodiment, one or more of the blades may include a heating mechanism toprovide an enhanced method of drying the solid protein product. Theheating mechanism may be a part of the heating system 220.

In a separate embodiment, microwave radiation may be employed as analternate method for drying the solid product. Microwave radiation hasbeen shown to provide more uniform drying while reducing damage to theproduct otherwise due to conventional heating mechanisms.

The FDR tank 200 may include a secondary agitator assembly 250. Like theprimary agitator assembly 230, the secondary agitator assembly 250 ispreferably located partially inside and partially outside of the FDRtank 200. The secondary agitator assembly 250 may be a high shearagitator for facilitating mass transfer during the reaction phase of amixture in the FDR tank 200. The secondary agitator assembly 250includes a driver 251 that is, at least in part, preferably locatedoutside of the FDR tank 200. It communicates with a rotatable shaft 252,which is preferably located inside or substantially inside the vessel210. The shaft 252 may include one or more arms 253 and one or morecorresponding blades 254. Although the secondary agitator assembly 250appears to be arranged in FIG. 2 in a vertical orientation, it may, inthe alternative, be arranged at any angle relative to the FDR tank 200.

Preferably, the FDR tank 200 also includes a vacuum system 240 capableof drawing a vacuum within the FDR tank 200. The vacuum system 240includes a vacuum pump 241 to reduce the air pressure in the FDR tank200.

Discharge of the final bulk solids from the FDR is preferablyaccomplished by using a pneumatic conveying system. This system avoidsthe need for manual removal of the product from the FDR. The pneumaticconveying system facilitates discharge of the solid protein product fromthe FDR to a final bulk container, such as a tote bind or a highstrength woven sack.

The FDR system is a highly automated system that utilizes a state of thePLC (Programmable Logic Controller) or similar logic processor. Highspeed input and output signals are integrated as part of the automationto permit the control system to rapidly respond to process deviationsand automatically return the process to within specification. Thecomplex mechanical nature of the FDR requires critical safetyinterlocks, and the automated system's logic processor scans theseconditions on a continual basis to ensure that the FDR equipment andauxiliaries are protected. Customized programming of the logic processorpermits the implementation of various software library modules that canbe deployed depending on the requirements of the process. For example,different animal tissue feed stocks may require slightly differentprocessing conditions in order to yield high quality protein product.The nature of the automation process will permit the implementation of arecipe driven system that can be tailored to various feed stocks andrelated processing conditions.

In another embodiment, the automated system used for the production ofprotein shall conform to a hierarchical model that combines processautomation with Business Intelligence (BI) involving ManufacturingExecution Systems (MES) encompassed by an overarching EnterpriseResource Planning (ERP) system. The Instrumentation, Systems andAutomation (ISA) S95 standard establishes a four tier hierarchical modelfor a manufacturing enterprise network. It characterizes genericapplication software and network architectures for manufacturing controlsystems as described under Table 1. The primary protein productionprocess occurs at Level 0 with Level 1 instrumentation that monitors theprocess operating parameters within specification. Level 2 comprises thelogic controllers, which may include a combination of PLC, DCS or SCADAsystems. These Level 2 logic processors contain the proprietary sourcecode and application recipes that define the protein production process.Since the Enterprise Control System is by definition a networkedstructure, information and data derived from the process and Levels 1and 2 are transferred to Level 3 material planning and quality systems.Level 3 is the repository for raw material and finished goods analyticaldata as well as inventory levels. Level 4 is the final repository forall information related to the protein manufacturing operations. Level 4analyzes internal manufacturing data and couples it against externalmarketing an forecasting information in order to optimize the schedule,raw material usages, and finished goods inventories.

TABLE 1 SA95 Enterprise Control System Integration Hierarchy SA95 LayerFunction Description Level 4 ERP Enterprise Resource Planning CRMCustomer Relationship Management APO Advance Planning Optimization Level3 MES Manufacturing Execution Systems LIMS Laboratory InformationManagement Systems CMMS Calibration Maintenance Management Systems WMSWarehouse Management Systems Level 2 PLC Programmable Logic ControllersDCS, BAS Distributed Control Systems, Building Automation Systems SCADASupervisory Control and Data Acquisition Level 1 Devices Processmeasurements and terminal control equipment Level 0 Process The physicalmanufacturing process

FIG. 3 illustrates a recovery system 300 (also indicated by referencenumeral 100 and used interchangeably throughout) in greater detail inaccordance with exemplary embodiments of the present invention. Moreparticularly, FIG. 3 illustrates the SLR system 370 in detail (alsoindicated by reference numeral 370 in FIG. 2 and used interchangeablythroughout). In addition to the detailed features illustrated in FIG. 3,the recovery system 300 may further include such features as aircompressors and nitrogen systems, for example, to maintain an inertenvironment inside the aforementioned filtration and storage tanks,depending on the type of organic solvent(s) used. The recovery system300 may also employ sensors for detecting explosive conditions andcorresponding alarms to indicate, for example, that the concentration oforganic solvent vapors exceed permissible threshold limits.

Turning attention back to FIG. 3, the SLR system 370, as mentioned,comprises a filtrate tank 371, although more than one tank isconceivable (see filtrate tank 372). The filtrate tank 371 may belocated upstream of one or more filters 373. The filters 373 help removeresidual solids from the filtrate (i.e., the solvent, liquid and oilmixture). The filters 373 may be located anywhere in the SLR system 370as required for the removal of the residual solids.

The SLR system 370 may also include a distillation unit 375, such as afractional distillation tower or WEE, (wiped film evaporator).Distillation unit 375 operates to recover fats/oils from the organicsolvent/water. Distillation unit 375 may be located downstream of thefiltrate tank 371. Pumps and blowers may be employed as necessary fortransferring the various liquids downstream for further processing. TheSLR system 370 may include more than one distillation unit, if needed.

The SLR system 370 preferably includes an ozone generator 374. As shownin FIG. 3, the ozone generator 374 is located downstream of the filtratetank 371, and it reacts with and neutralizes amines in the filtrate,thereby eliminating the odor (e.g., fishy odor) associated with theamines. Odors associated with fish are due to the natural process ofdecay. Bacterial enzymes attack the flesh of fish, and this triggers anoxidation reduction reaction. The muscle of the fish which containstrimethylamine oxide (TMAO) breaks down by decomposition, thus producingtrimethylamine and dimethylamine. These two amines give rise to thecharacteristic fishy odor. Thus, the ozone removes this odor bydestroying the molecules, bacteria, and spores that cause unpleasantsmells. Triatomic oxygen is ozone. In a reverse reaction using Ozone,the third oxygen atom attaches itself to the amine molecules andultimately renders them odorless. The ozone generator 374 can be alsolocated at other part of the SLR system 370 where deodorization isneeded.

Deodorization of the solvent and liquid products are further achievedthrough the use of in-line activated carbon filters. Activated carbon isa well established material for removal of organic contaminants from aprocess stream. The benefit of using activated carbon in the SLR processis that trace amines are further eliminated along with the associatedodor attributed to the fishy amine smell.

The SLR system 370 may include condensers downstream of the distillationunit 375 to recover water and organic solvent. Further processingequipment may be required as necessary to obtain purified water. Thepurified water may then be transferred to a recovery tank 396.

The SLR system 370 may further include one or more distillation units380 to recover purified animal oil (e.g., omega-3 oil). Preferably, thedistillation unit 380 may contain a phase separation apparatus. Thedistillation unit 380 is located downstream of the distillation unit375. The distillation unit 380 generally separates the animal oil fromwaste solid fat. The distillation unit 380 may, for example, be a ThinFilm Evaporator (TFE), Wiped Film Evaporator (WFE) or a moleculardistillation unit. Specifically, a molecular distillation unit, may beemployed to recover a purified omega-3 oil from waste solid fat. Variousgrades of purity may be achieved and techniques readily known in the artmay be employed to achieve a final grade of omega-3 oil. Oil may betransferred to a recovery tank 397 while residues are captured in a tank398.

Referring back to FIG. 3, recovery system 300 may include a controller391. The controller 391 may include an electrical motor control center.The controller generally provides the operator with an interface throughwhich the operator can achieve real-time, automated control over thevarious components and subsystems that make up recovery system 300. Thecontroller 391 may, for example, communicate with and/or provide controlover tank volumes, temperatures, device states, sensors and alarms.

The system 300 may further include one or more grinders 305. Thegrinders 305 are preferably made of stainless steel construction andconfigured to grind raw animal tissue feedstock, such as fish, into ¼″to ½″ cube sizes. The grinders 305 are located upstream of the FDR tank310, such that the grinders 305 grind animal tissue feedstock receivedfrom the animal tissue feedstock storage tank/room 301 into smallerparticles, as specified above, for further processing.

After the animal tissue feedstock is ground, the feedstock may becombined with an organic solvent for preparing a homogenized slurry ormixture. As shown in FIG. 3, system 300 includes preparation tanks 330for combining the animal tissue feedstock and the organic solvent. Thepreparation tank 330 preferably processes up to 50 gpm. The preparationtank 330 may be a heated agitated tank. The preparation tank 330 is alsolocated upstream of the FDR tank 310. Level sensors and flowmeters maybe employed in or associated with the preparation tank 330, in order toprovide feedback information to the operator through controller 391, tohelp ensure adequate flow in accordance with operator preferences.

System 300 may also comprise a milling apparatus 350 and a solid productrecovery system 360. The milling apparatus 350 mills the solid productto obtain a granular or powder form of the recovered solid protein. Themilled product may further be cured in an oven. After curing, thefinished product is stored in a final product storage facility. Uponcompletion of these processes, the product with all of its proteinproperties, can be managed in such a way so as to give it physicalcharacteristics sufficient to allow it to be consumed and ingested bychildren and adults easily and without unpleasant flavors or odors whichhave a disagreeable impact or which give rise to rejection. For example,without limitation, the powder may be pressed into a solid pill form,placed in a capsule to be swallowed, or added to a liquid and consumedas a beverage. The recovered solid protein may then be collected by thesolid product recovery system 360.

Recovery system 300 also comprises an organic solvent recycle system390. Preferably, the solvent is isopropyl alcohol (IPA); however, itwill be readily apparent to those skilled in the art that solvents otherthan IPA may be used. As mentioned above, the organic solvent may bedistilled from the water by use of a heated still and condensers.However, once the solvent is removed from the water, the solvent may betransported back to a solvent storage tank 302. This recycled organicsolvent may or may not be combined with new or fresh solvent prior tobeing transferred to the FDR tank 310, where it will be combined withre-filtered wet cake, or transferred to preparation tank 330, where itwill be combined with the animal tissue. Refiltered wet cake is theresidual solid protein product that remains behind in the FDR followingeach reactor recycle process. Recall that once the raw fish/IPA mixtureis sent to the FDR tank 310. IPA is then filtered off and the filtrateis transferred to the solvent recovery system. Solid protein productremains behind in the FDR tank 310. Another charge of IPA is then sentto the FDR tank 310 where the solid protein product undergoes a secondreactor/heating/filtration cycle. IPA is once again filtered off leavingbehind the solid protein “wet cake”. This recycle process is conductedone more time for a total of 3 times. In general, the total number orrecycles will range from 1 to 4, and is determined by the final productdesired quality. The FDR tank 310 and preparation tank 330 may receiveone of the following with respect to organic solvent: entirely new(fresh) organic solvent, entirely recycled organic solvent, or acombination thereof. As is apparent, the solvent recycle system 390includes piping, as described above, for transporting the organicsolvent between the solvent recovery tank 395 of the SLR system 370, theorganic solvent storage tank 302 and the FDR tank 310.

The recovery system 300 may include a recovery tank 396 for collectingwater, a recovery tank 397 for collecting oils, including omega-3 fattyacids, and a residue discarding tank 398 for collecting residue. Stillfurther, recovery system 300 comprises a VOC recycling system 392 forcapturing emissions of fumes/vapors formed in the FDR tank 310. As shownin FIG. 3, for example, emissions exit the vessel FDR tank 310 via aport, and the vapors may be transferred to a fume condenser and chillerfor condensing the vapors into usable organic solvent. The condensedorganic solvent may be transferred via a solvent recycle line to theorganic storage tank 302 for reuse.

Process

According to an aspect of the present invention, a process is describedfor recovering products originally derived from animal tissue. In oneembodiment, solid protein product is recovered. In another embodiment,solid protein product in addition to water derived from animal tissueare recovered. In a further embodiment, solid protein product, water andanimal oil derived from the animal tissue are recovered.

Animal tissue, for the purposes of this application, is defined ashaving eukaryotic cells of various shapes and sizes. Animal cells arefurther characterized as excluding cell walls which are present in allplant cells. The animal tissue may include but is not limited to landand marine animals such as insects, fish, poultry and red meat. In anexemplary embodiment, the animal tissue feedstock contains fish. In yetanother exemplary embodiment, animal tissue feedstock is maintained attemperatures less than 50° F., preferably less than 45° F., and morepreferably less than or equal to 40° F., prior to being processed by thepurification system of this invention.

As stated, the animal tissue may be fish, and in particular, raw fish.The raw fish should be fresh and handled in a sanitary manner. Thequality of the raw material should also be verified. The fish is alsoground, as explained above (see e.g., mill 350), into pieces so as toform a fishmeal prior to mixing with organic solvent and furtherprocessing.

An organic solvent is generally employed in the process. The solvent mayinclude an alcohol, wherein the hydroxyl functional group is bonded to acarbon atom. In an alternative embodiment, the solvent may be selectedfrom those organic solvents with a volatile organic content (VOC)ranging between about 200-500 g/L. In still another alternativeembodiment, the solvent is selected such that it meets VOC regulationspromulgated by local governing authority. In a preferred embodiment, thesolvent, as stated, is IPA (isopropyl alcohol).

A mixture of fishmeal and solvent is initially heated; however, a lowheat is preferably used so there is no risk of decomposition of theprotein product due to thermal degradation. The mixture of fishmeal andsolvent should sufficiently be balanced so that the fishmeal dissolvesinto a viscous liquid during processing in the FDR tank, and inparticular, the heating process, which is done at a controlledtemperature by means of a variable control system that prevents thedestabilization of the which, in turn, would reduce or eliminate thepotency of the protein. The ratio of animal tissue to solvent will, ofcourse, depend on various factors including but not limited to thespecific animal tissue and solvent used. Where the animal feedstock israw fish and IPA is employed as the organic solvent, the ratio of fishin kilograms to IPA in liters ranges between about 1:1 to 1:2.2; 1:2.1;1:2.0; 1:1.9; 1:1.8; 1:1.7; 1:1.6; 1:1.5; 1:1.4; 1:1.3; 1:1.2; and1:1.1. More preferably the ratio is about 1:2. In a preferred,commercial embodiment of the present invention, upon scale-up, about5,000 Kg of raw fish and about 10,000 L of organic solvent are combinedto form the mixture of fishmeal and solvent.

As illustrated in FIGS. 1-3, the mixture of animal tissue and organicsolvent is fed, e.g., via a screw conveyer from the preparation tank(e.g., see preparation tank 330) to the FDR tank (see e.g., FDR tank310), where it is heated, with agitation at a temperature rangingbetween 45-75° C. for approximately 2 hours in the FDR tank. The primaryagitator assembly, as discussed above, ensures uniform heating andprevents decomposition of the animal tissue and organic solvent mixture,particularly that portion of the mixture in proximity of the walls orbottom of the compression vessel. In doing so, protein with a highconcentration is recovered, specifically with 85% or higher pureprotein, as characterized through a complete aminogram. An aminogram isa collection of amino acids present in a product depending on the typeof animal tissue. The recovered protein may be a complete aminogram,non-hygroscopic, and substantially free, of fish odor or smellcontributed by amines. The recovered protein may also be non-hygroscopicand sterile, and visually, the protein, may exhibit a cream color.

The animal tissue may be fed by a screw conveyer to a preparation tank(see e.g., preparation tank 330). The organic solvent is then added toensure an adequate mixture is formed prior to being fed to the FDR tank(see e.g., FDR tank 3). The preparation tank may also include anagitator, as well as a jacketing and insulation system to permitexternal heating and cooling. Preferably, the mixture is heated to atemperature not exceeding 75° C., for example, about 45-50° C. Theresulting homogeneous mixture is then fed to the FDR tank.

In the FDR tank, the homogeneous mixture is again heated and agitated,then filtered. The residual protein wet-cake is then dried, preferablyusing heat and vacuum or microwave. By so doing, several unit operationsare condensed into a single piece of equipment. Namely, slurry vessels,product centrifuges/filtering mechanisms, stand-alone dryingapparatuses, along with accompanying valves, conduits, blowers, pumps,sensors, controllers, and the like, that assist with the transfer of themixture between each operation are not required. As a result, productioncycle time for recovering product, such as for example solid protein,significantly is reduced. Within the FDR tank, the process generally isautomated and operates in closed circuit, e.g., closed system.

After the mixture is heated and agitated for a period of approximately 2hours, as mentioned above, the FDR tank operates in a filtration mode.The filtrate including the organic solvent is discharged from the FDRtank to the SLR system. A wet cake is retained in the FDR tank. The FDRtank then operates in heating/drying mode under full vacuum at atemperature not exceeding 80° C., for example, from about 50-80° C. for1 hour to 10 hours to recover solid.

After filtration, one or more heating, agitation and filtration cyclesmay be employed. For each additional heating, agitation and filtrationcycle, organic solvent is fed into the FDR tank. As explained above, thesolvent may be new (fresh) solvent, recycled solvent recovered from theSLR system, or a combination of both. The recycled solvent may betransferred from the SLR system through the use of a solvent recyclesystem (see e.g., solvent recycle system 390) to the solvent storagetank (see e.g., solvent storage tank 302), thus promoting greenmanufacturing initiatives. After the above-mentioned one or moreheating, agitation and filtration cycles, the FDR tank operates inheating/drying mode under full vacuum at a temperature ranging fromabout 50-80° C. for 1 hour to 10 hours to dry and recover solid proteinfrom the solid portion of the mixture retained in the FDR tank.

The recovered solid protein is ultimately discharged from through anoutlet port in the FDR tank to a storage tank. The solid protein may bereviewed and analyzed by quality control to ensure adequate yield ofprotein. In an exemplary embodiment, the solid protein is present in ayield of about 15-25 wt. % based upon the animal tissue entering the FDRtank 110. Preferably, the yield is greater than about 18 wt. % solidprotein recovered from animal tissue entering the FDR tank 110.

A laboratory analysis of the recovered solid protein from the systemexhibited protein concentrations in the range of about 85-95%. Thequality of the final product is generally excellent at least because theproduct is not degraded as the process is low temperature, e.g., notgenerally exceeding 80° C., in order to prevent thermal degradation ofthe protein. Hence, the organoleptic structure is maintained resultingin a relatively complete amino gram on the high quality concentration ofprotein on the final product. The product exceeds all FDA requirementsfor a supplement and is an excellent product for world food needs. The35 gram serving provides sufficient protein to meet a person's aminoacid requirement like a full meal. The most frequently used methods formaking these determinations at the protein level, are electrophoresisand thin layer chromatography; and it has been possible to demonstratethat there exists at least one specific protein for each species.

The recovered protein also has a long shelf life defined as maintaininga fairly constant profile over a long period of time. In one embodiment,the recovered solid protein product was tested in a laboratorysimulating environmental conditions over 10 years. The constant profilemay be attributed to the product's non-hygroscopic, or substantiallynon-hygroscopic nature. That is, the recovered, solid protein does notabsorb humidity or grow any bacteriological processes in view of the lowmoisture content. Preferably the moisture content is less than about 8wt. % of the recovered, solid protein.

The recovered protein has amino acid compositions that are balanced toafford a nutritionally advantageous characteristic. The recoveredprotein may also be sufficiently stable and sterile, i.e., substantiallyor entirely 100%.

Further, in accordance with the process of the present invention, thefiltrate (i.e., the heavy liquids) that are extracted as a result of thefiltering in the FDR tank is transferred to the SLR. The filtrate mayinclude but is not limited to oils, fats, solvent and water. When theanimal tissue is fish, the oil may include omega-3 fatty acids. In theSLR system, the filtrate may first be transferred to a filtrate tank(see e.g., filtrate tank 371), and subsequently filtered once again (seee.g., filter 373) to remove residual solids. Alternatively, the filtratemay directly be transferred to a solvent recovery or distillation tower(see e.g., distillation unit 375), in order to separate the organicsolvent/water from oils/fats. As previously stated, the solvent may betransferred to a recovery tank 395, and thereafter, employed as recycledorganic solvent. The water may be transferred to a recovery tank 396 andpurified further as necessary.

The recovered oils, for example, omega-3 fatty acids, may be filtered toremove residue (see e.g., filter 373) and to increase the puritythereof. It may also be treated with ozone to remove the odor byneutralizing any amines present in the oil. The residue may betransferred to a discarding tank (see e.g., residue discard tank 398).The oils, including omega-3 fatty acids, may be transferred to a firstrecovery tank (see e.g., recovery tank 397). There, the oil may undergofurther purification, as required, according to a further embodiment andtransferred to another recovery tank 397 b. The recovered oils includingomega-3 fatty acids are polyunsaturated fatty acids with a double bondon the end of the carbon chain. They are considered essential fattyacids. Humans cannot readily make omega-3 fatty acids in their bodies,and therefore it must be obtained from other sources since they play animportant role for normal metabolism.

In an exemplary embodiment, omega-3 fatty acids are recovered in amountsgreater than or equal to about 5% of the original animal tissuefeedstock (whereby 1 L=0.96 Kg). Preferably omega-3 fatty acids arerecovered in amounts of greater than or equal to 6% of the originalanimal tissue feedstock, More preferably, omega-3 fatty acids arerecovered in amounts greater than or equal to 7% of original animaltissue feedstock. [811 L/2*0.96=389 kg].

In yet another embodiment, the organic solvent/water may independentlybe recovered by employing extractive distillation. Namely, a thirdcomponent is introduced into the process. For example, when isopropylalcohol (IPA) is the organic solvent, diisopropyl ether (IPE) may beemployed whereby IPA and IPE combine to completely separate watertherefrom. The water is recovered at outlet 396 and may be furthersubjected to another ozone treatment. In still another exemplaryembodiment, distilled water is recovered in amounts less than or equalto about 35% of the initial liquids portion entering the SLR system 37.Preferably, water is recovered in amounts less than or equal to about30% of the liquids portion entering the SLR system 370. More preferably,water is recovered in amounts less than or equal to about 25% of theliquids portion.

On the other hand, the IPA/IPE mixture is then further distilled in asecondary distillation column to recover IPA. The IPA may be transferredto a recovery tank 395 for further processing as discussed above.

RESULTS AND EXAMPLES

The following examples illustrate specific aspects of the presentinvention. The examples are not intended to limit the scope of thepresent invention. Test results may vary for different types of fishspecies, but the method and system are applicable to all fish species.Table 2, as shown below, describes the composition an amino gram ofsolid, protein powder recovered from fish according to an embodiment ofthe present invention. Specifically, the yield of protein is 85.4%,moisture is 7.68%, crude fat is 1.42%.

TABLE 2 CERTIFICATE OF ANALYSIS Sample Identification Sample #: 05-5432Advance Protein Powder, Serving = 35 g Method: B0202: Amino Acid Profile(Total) by AOAC 98170 PB100 NLEA Abbreviated Nutrient Package(Proximate) Results: OF AMINO GRAM Sample #05-5432 Theoretical Test /100g Serving Units Level Protein − Food 85.4 29.9 grams 85-90% Protein =Nitrogen × 6.38 Ash 9.20 3.22 grams Moisture By Vacuum Oven 7.68 2.69grams Crude Fat By Acid Hydrolysis 1.42 0.497 grams 0.5% CaloriesCalculated 340 119 calories Total Amino Acid Profile Tryptophan 1.060.371 grams Cysteine 0.83 0.291 grams Methionine 2.51 0.879 gramsAspartic Acid 4.58 1.6 grams Threonine 2.15 0.753 grams Serine 1.640.574 grams Glutamic Acid 6.64 2.32 grams Proline 1.89 0.662 gramsGlycine 2.54 0.889 grams Alanine 2.9 1.015 grams Valine 2.31 0.809 gramsIsoleucine 2.03 0.711 grams Leucine 3.51 1.23 grams Tyrosine 1.54 0.539grams Phenylalanine 1.86 0.651 grams Lysine, Total 3.92 1.37 gramsHistidine 1.22 0.427 grams Arginine 2.97 1.04 grams

As shown in Table 2, specific tests conducted on the recovered solid,protein powder derived from fish. As shown, the protein has over 98%digestible protein according to the well-known Pepsin test (0.2%Pepsin). Pepsin is a material that is used to digest protein structures.The Pepsin test is used to determine how much protein is within amixture. The test involves analyzing the amount of protein that wasdigested, then back calculating that amount to the original quantity ofprotein material in the sample undergoing analysis. The trans fatty acidisomers are less than 0.1 wt. %, and preferably less than 0.05 wt. %.The amount of cholesterol is less than 0.1 wt. %, preferably less than0.05 wt. %, and more preferably less than 0.02 wt. % of a 100 g serving.

TABLE 2 CERTIFICATE OF ANALYSIS Sample identification: Sample #: 05-5432Advance Protein Powder, Serving = 35 g Method: B0003: CustomizedAnalyses (Pepsin (0.2%) Digestible Protein) B7033: Cholesterol by GasChromatography (GC), AOAC 994.10 00201: Total Trans Fatty Acid by GasChromatography (GC), AOAC 996.06 Results: Sample #05-5432 Test /100 g/Serving Units Pepsin (0.2%) Digestible Protein 98.1 34.3 grams TotalTrans Fatty Acid Isomers 0.02 0.007 grams Cholesterol 0.0173 0.00605grams

As shown in Table 3 below, an elemental scan of the solid protein powerindicates the following elements present in mg per serving. Also shownbelow in Table 3 is the amount of each element in parts per million.

TABLE 3 CERTIFICATE OF ANALYSIS AMINOGRAM Sample Identification: Sample#: 05-5432 Advance Protein Powder. Serving = 35 g Method: AL194:Elemental Scan (65) by ICP MS Results: Sample #05-5432 Test ElementalResult (mcg/serving) Result (ppm) Lithium <35 <1 Boron <35 <1 Magnesium56,000 1,600 Phosphorus 220,000 6,400 Calcium 770,000 22,000 Titanium 772.2 Chromium 91 2.6 Iron 4,600 130 Nickel <35 <1 Zinc 2,070 59 Germanium<35 <1 Selenium 91 2.6 Strontium 3,900 110 Zirconium <35 <1 Molybdenum<35 <1 Rhodium <35 <1 Silver <35 <1 Indium NA NA Antimony <35 <1 Cesium<35 <1 Lanthanum <35 <1 Praseodymium <35 <1 Beryllium <35 <1 Sodium70,000 2,000 Aluminum 2,000 56 Potassium 190,000 5,500 Scandium <35 <1Vanadium <35 <1 Manganese 120 3.3 Cobalt <35 <1 Copper 160 4.7 AdvanceInternational Corporation Test Result (mcg/serving) Result (ppm) Gallium<35 <1 Arsenic <35 <1 Rubidium 49 1.4 Yurium <35 <1 Niobium <35 <1Ruthenium <35 <1 Palladium <35 <1 Cadmium <35 <1 Tin <180 <5 Tellurium<35 <1 Barium 63 1.8 Cerium <35 <1 Neodymium <35 <1 Samarium <35 <1Gadolinium <35 <1 Dysprosium <35 <1 Erbium <35 <1

Table 4 shown below compares the nutritional content for 25 mg proteinof one example of the recovered solid protein of the inventive processand system which subsequently has been milled into a powder “APP” versus25 mg protein of commercial products on the market. APP is derived fromfish. Specifically, APP has fewer calories than each of the commercialproducts except for NB soy. APP has fewer carbohydrates and fat than NBsoy. Compared with JF soy, APP has fewer calories and less fat. Comparedwith each DFH whey, JF whey, GNC whey, Whey isolate and Wheyconcentrate, APP has fewer calories, carbohydrates, fat, saturated fatand cholesterol.

TABLE 4 Standardized to 25 grams of protein per serving DFH JF GNC WheyWhey JF NB APP whey whey whey isolate concentrate soy soy Calories 100135 131 135 113 125 110 91 Protein 25 g   25 g   25 g   25 g  25 g   25g  25 g  25 g Carbohydrate  0 g    3 g    3 g  4.2 g 2.8 g  3.1 g   0 g0.7 g Fat  0 g  2.1 g  1.4 g  2.1 g 0.7 g  1.6 g 0.9 g 0.2 g SaturatedFat:  0 g  2.1 g  2.3 g  1.0 g 0.5 g  1.0 g   0 g   0 g Cholesterol  0 g31.3 mg 69.4 mg 72.9 mg 2.8 mg 64.6 mg   0 g   0 g

Table 5 shown below compares chemical elements existing in 25 mg of oneexample of the recovered solid protein of the inventive process andsystem which subsequently has been milled into powder “APP” versus 25 mgprotein of commercial products on the market. APP is derived from fish.Notably, the calcium, iron and zinc contents of 25 mg APP issignificantly greater than for each of DFH whey, JF whey, GNC whey, WheyIsolate, Whey concentrate, JF soy and NB soy. The amount of iron presentin APP is significantly greater than in each of DFH whey, JF whey, GNCwhey, Whey isolate, and Whey concentrate.

TABLE 5 Comparing mineral content per 25 grams of protein as apercentage of the RDA DFH JF GNC Whey Whey JF NB APP whey whey wheyIsolate concentrate soy soy Calcium   55% 12.5% 9.0% 8.3% 18.8%  2.9% 5.0% Iron 18.1%  4.2% 1.8% 22.2% 22.2% Magnesium   10%   3.5%  2.8%Zinc  9.8%    6.7% Sodium  2.1%  2.0% 1.7% 2.6%   2%  2.3%  0.6%Potassium  4.6%  4.6% 3.7% 5.7% 8.7%  3.7% 10.6% 12.9% Phosphorus 18.4%21.3% 8.9% 29.3%,

1. A method for recovering protein powder meal, crude and pure omega-3oil and purified distilled water from animal tissue comprising: a.providing a first mixture of animal tissue and an organic solvent; b.feeding the animal tissue and the organic solvent to a single, unitaryfilter-drier-reaction tank; c. agitating and heating the first mixtureof the animal tissue and the organic solvent in thefilter-drier-reaction tank; d. removing a liquid portion of the firstmixture including the organic solvent from the filter-drier-reactiontank to recover the purified distilled water and the pure omega-3 oilwhile retaining a solid portion of the first mixture therein; e.recycling the organic solvent; and f. baking the retained, solid portionto recover the protein powder meal.
 2. The method according to claim 1,wherein the animal tissue includes raw fish.
 3. The method according toclaim 2, further comprising: recovering pure omega-3 oil from theremoved liquid portion of the first mixture through the use of moleculardistillation in combination with wiped film evaporation (WFE).
 4. Themethod according to claim 1, further comprising: recovering water fromthe removed liquid portion of the first mixture.
 5. The method accordingto claim 1, further comprising: feeding additional organic solvent tothe filter-drier-reaction tank before the baking step; agitating andheating a second mixture including the retained, solid portion of thefirst mixture and the additional organic solvent in thefilter-drier-reaction tank; and removing a second liquid portion fromthe second mixture while retaining a solid portion of the second mixturein the filter-drier-reaction tank.
 6. The method according to claim 5,wherein the additional organic solvent includes recycled organic solventderived from the removed liquid portion of the first mixture.
 7. Themethod according to claim 5, wherein the additional organic solventincludes recycled, condensed vapor of the organic solvent fed to thefilter-drier-reaction tank.
 8. The method according to claim 1, whereinthe animal tissue and the organic solvent are fed to thefilter-drier-rector tank in a ratio ranging from about 1:1 to 1:2.2. 9.The method according to claim 1, wherein the recovered solid protein isgreater than 18 wt. % of the animal tissue fed to thefilter-drier-reaction tank.
 10. The method according to claim 1, whereinthe recovered solid protein has less than about 8 wt. % humidity. 11.The method according to claim 1, wherein the recovered solid protein hasgreater than about 80% concentration of protein.
 12. The methodaccording to claim 11, wherein the recovered solid protein has less thanabout 90% concentration of protein. 13.-25. (canceled)
 26. A proteinproduct, wherein said protein product: (a) is non-hygroscopic; (b)comprises non-degraded protein; (c) comprises a complete aminogram; and(d) comprises 80-95% of protein by weight.
 27. The protein product ofclaim 26, wherein the protein product is in a powder form.
 28. Theprotein product of claim 26, wherein the protein product is in agranular form.
 29. The protein product of claim 26, wherein the proteinproduct has over a 10 year shelf life.
 30. The protein product of claim26, wherein the protein product does not support bacterial growth. 31.The protein product of claim 26, wherein the protein product is sterile.32. The protein product of claim 26, wherein the protein product isrecovered from animal tissue.
 33. The protein product of claim 32,wherein the animal tissue is any part of a fish.
 34. The protein productof claim 33, wherein the part of the fish ordinarily considered waste.35. The protein product of claim 26, wherein the protein product issubstantially free of odor or smell contributed by amines.
 36. Theprotein product of claim 26, wherein the protein product comprises anorganoleptic structure.
 37. The protein product of claim 26, wherein theprotein product comprises 1.42% of crude fat by weight.
 38. The proteinproduct of claim 26, wherein the protein product comprises 7.68%moisture by weight.
 39. The protein product of claim 26, wherein theprotein product comprises over 98% digestible protein.